TW200911975A

TW200911975A - Reaction zone comprising two risers in parallel and a common gas-solid separation zone, for the production of propylene

Info

Publication number: TW200911975A
Application number: TW097123545A
Authority: TW
Inventors: Thierry Gauthier; Vincent Coupard; Jan Verstraete; Romain Roux
Original assignee: Inst Francais Du Petrole
Priority date: 2007-06-27
Filing date: 2008-06-24
Publication date: 2009-03-16
Also published as: FR2918070B1; KR101531430B1; US8491781B2; WO2009007519A3; WO2009007519A2; KR20100040738A; TWI450955B; CN101687130A; US20100286459A1; JP2010531378A; FR2918070A1; CN101687130B; JP5253503B2

Abstract

The present invention describes a reaction zone comprising at least two fluidized reactors, a principal reactor for cracking a heavy hydrocarbon cut, the other, additional, reactor for cracking one or more light cuts, the effluents from the two reactors being treated in a common gas-solid separation and quench zone. Performance is enhanced because the thermal degradation reactions in the reaction zone are controlled in an optimum manner.

Description

200911975 九、發明說明：【發明所屬之技術領域】催化裂化法（F C C)可藉由在酸催化劑存在下裂化重饋料分子而將具有一般超過3 4 〇 t之沸點之重烴饋料轉化為較輕烴館份。 CC法主要產生油及lpg(液化石油氣）以及表示為 LCO及HCO之較重镏分。 ^ FCC關聯產*(co_product)t之一種為丙烯，發現丙烯中存在大量LPG。可自經生產以供應石油化工聯合企業之其他氣體分離丙烯。多年來，丙烯需求大幅增加促使產生藉由催化裂化產生愈來愈多丙稀之精煉機。一種已知解決方案係由將比主要饋料輕且較佳地含有大量一般具有5個或5 個以上奴原子（表示為C5=+)之長鏈烯烴的烴餾***化組成，該餾分係源自藉由以FCC裂化重饋料而產生之汽油，或源自C4=+烯烴募聚單元，或源自產生長鏈烯烴之任何其他方法。200911975 IX. Description of the invention: [Technical field to which the invention pertains] The catalytic cracking process (FCC) can convert a heavy hydrocarbon feed having a boiling point generally exceeding 3 4 〇t into a heavy hydrocarbon feedstock by cracking heavy feed molecules in the presence of an acid catalyst. Lighter hydrocarbons. The CC method mainly produces oil and lpg (liquefied petroleum gas) and a heavier weight expressed as LCO and HCO. ^ One of the FCC-related products* (co_product) t is propylene, and a large amount of LPG is found in propylene. The propylene can be separated from other gases produced by the petrochemical complex. Over the years, a significant increase in demand for propylene has led to the creation of more and more propylene refiners by catalytic cracking. One known solution consists of splitting a hydrocarbon fraction which is lighter than the main feed and preferably contains a large number of long-chain olefins generally having 5 or more slave atoms (denoted as C5=+), the fraction system It is derived from gasoline produced by cracking heavy feed with FCC, either from a C4 = + olefins recruitment unit, or from any other process that produces long chain olefins.

J 彼裂化可在與加工重烴饋料之反應器相同之反應器中進订，或在更有利操作條件下於專用反應器中進行，以產生大量丙烯。本發明之目標為描述可將來自轉化重餾分之反應器之排出物的分離與源自專用於轉化輕餾分之一或多個反應器之排出物的分離整合之反應區。、、°果為改良重餾分轉化反應器之功能，因為使此反應器中之稀釋相氣體循環保持在控制下且不再必需以蒸汽沖洗 131895.doc 200911975 此低循環區來消除死區（dead zone)。本發明亦有利地使得使用輕餾分轉化反應器之驟冷來驟冷來自重餾分轉換反應器之排出物。在本文之其餘部分中，為使用熟習此項技術者之術語學’將呈伸長管形式且使用傳輸床操作之流體化床催化裂化反應器稱作豎管。此術語一般描述氣流及催化劑流為上升平仃流之反應ϋ。亦可能於以傳輸床模式操作，但氣體及催化劑以下向流流動之相同伸長管狀反應器中進行反應在本文之剩餘部分中，為簡單起見使用術語"登管”，此術語包括以滴管操作之可能性。來自重餾分FCC單元之主要饋料一般為烴或亦 -ir a -X. ___ . .....认1力工叹土 I (亦即 >、_)含有具有超過3贼之沸點之分子的烴之混合物。此饋料含有有限量之金屬(Ni，，一般小於5〇ppm，較佳地小㈣PPm，及-般大於_量％之氫含# 限制於低於0.5重量%亦為較佳的。 …里 ^t^#^,(c〇nrads〇n carbon).t(^ as™ D 482定義）在較大程度上碎定用 FCC單元的尺寸。疋…十衡之視饋枓令之康拉特遜碳而定須特定化以滿足敎平衡田… 丰L…尺寸必 3重量。/，削τ: 饋料之康拉特遜碳小於重里則可能操作FCC單元，其化床中之^來滿足_衡。 ’u燒流體重量％康拉特遜碳之其他解決方案，可對於具有超過3 應用可滿足熱平衡之較重饋料而言，諸如部分燃燒再生 131895.doc 200911975 不存在空氣下之部分再生與過量空氣下 R2R過程之雙重再生。之再生的組合；或J. Cracking can be carried out in the same reactor as the reactor for processing heavy hydrocarbon feeds, or in a dedicated reactor under more favorable operating conditions to produce a large amount of propylene. The object of the present invention is to describe a reaction zone in which the separation of the effluent from the reactor for converting the heavy fraction can be integrated with the separation from the effluent dedicated to the conversion of one or more of the light ends. ,, is the function of the modified heavy fraction conversion reactor, because the dilution phase gas circulation in this reactor is kept under control and it is no longer necessary to flush with steam. The low circulation zone is used to eliminate the dead zone (dead) Zone). The invention also advantageously allows quenching using a light ends conversion reactor to quench the effluent from the heavy fraction conversion reactor. In the rest of the text, a fluidized bed catalytic cracking reactor, which is in the form of an elongated tube and operated using a transfer bed, is referred to as a standpipe for the use of the terminology of those skilled in the art. This term generally describes the reaction enthalpy of the gas stream and the catalyst stream as a rising turbulent flow. It is also possible to operate in the transport bed mode, but the gas and the catalyst are reacted in the same elongated tubular reactor flowing downstream. In the remainder of the text, the term "pipe-pipe is used for simplicity, and the term includes Possibility of pipe operation. The main feed from the heavy fraction FCC unit is generally hydrocarbon or also -ir a -X. ___ . . . .. 1 力工叹 I I ( ( ( ( ( a mixture of hydrocarbons of molecules having a boiling point of more than 3 thieves. This feed contains a limited amount of metal (Ni, generally less than 5 〇 ppm, preferably small (four) PPm, and - generally greater than _ % by weight of hydrogen containing # is limited to low It is also preferred to use 0.5% by weight. ... ^^^^^^(c〇nrads〇n carbon).t(^ asTM D 482 defines) The size of the FCC unit is determined to a large extent. ...the ten-equal vision of the Conradson carbon must be specified to meet the balance of the field... Feng L... size must be 3 weights. /, cut τ: Conradson carbon of the feed is less than heavy Operate the FCC unit, which is used in the chemical bed to meet the balance. 'u burning fluid weight % Conradson carbon other solutions, can be Application of more than 3 can satisfy the heat balance of the heavier feed was concerned, such as partial combustion regeneration composition 131895.doc 200911975 double R2R process of reproducing the lower portion of regeneration air with an excess air at the absence of regeneration;. Or

,、工再循％之裂化餾分注射至汽化時吸收餘熱之豎管中 :為滿足熱平衡之可能的解決方案。最後，將交換器(在在項技:中一般稱作催化冷卻器）置於再生區中可（例如）藉產生热氣且冷卻催化劑來吸收部分餘熱。藉由使用一或多種以上技術，可能藉由催化裂化轉化具於15重里％，較佳小於1〇重量％之康拉特遜碳之重餾重館分之催化裂化產生介於乾氣與轉化殘餘物範圍内之排出物。以下餾分係分類為排出物，且通常隨其組成或其彿點變化而經定義： •乾燥及酸性氣體（主要為：H2、h2S、ci、C2); •含有C3-C4分子之液化石油氣； 3有具有小於220 C (標準餾出點（standard eut p〇int)) 之沸點之較重烴的汽油； •具有標準220-360。。沸點範圍之柴油，其為高度芳族的且因此稱作LCO(輕循環油）； •轉化殘餘物，其具有超過36〇t：2沸點。可記使彼等餾分中之某些再循環以使其再次催化裂化。亦可能使由FCC直接產生之餾分或由FCC產生，但經受 ik後轉化之餾分再循環。舉例而言，可能使具有之沸點範圍且富含烯烴之來自FCC的輕汽油裂化以利於產生丙稀。 131895.doc 200911975 了此自排出物分離富含c4_C5分中之、说！·- — π 刀子之餾分以使彼餾分烯烴券聚且接著裂化寡聚物。亦可能設法回收LCO，使t气作餾分去時展頦P亡〃風化，接著裂化彼餾分，彼夕"展見更有利於催化裂化之經改質特性。夕種組合均為可能的。亦他方土土 J j月匕口又法向FCC_注射源自其方去之輕餾分以將其催化轉化！^ 口此，例如可能設法催 W化石油化學石腦油。亦可能設法催化裂化源自植分祖物求源或動物來源之輕烴餾 μ 4饋料係由主要含有甘 '，由一 l 女3虿甘油二3曰及脂肪酸或酯之所有植物油及動物脂肪構成，其，、τ心如肪鏈含有6至25個碳原于°此等油可為非洲油、於納杳，丄籽m山搁實油、椰幹油、萬麻油或棉化生，由、亞麻仁油及芥薺油、s 丨龄/由胡妥油及源自（例如）向日癸或油菜籽或藉由遺傳修飾或雜交產生之任何油。亦了使用油炸油、各種動物油(諸如魚油卜動物脂或板匕等饋料4乎無或完全無不含芳族烴之含硫及含氮化合物。、和也此類饋料、植物油或動物脂肪在用於本發明方、、⑴最初可經文使用合適處理之預處理或預精煉步驟以 /肖除各種污染物。使定義為3有至少80重量％的具有小於340T：之沸點之分子且包括先刖段落之植物油及動物脂肪之輕餾分催化裂化可顯著改變重餾分FCC之產率結構：首先轉移選擇性。舉例而言，藉由使接著經裂化之 131895.doc 200911975 C4-C5餾分募聚來進rC4_C5餾分之間接轉化以產生富含烯烴之C3餾分； •其次’所注射之輕館分之反應熱量藉由吸熱改變單元之熱平衡’其由於所形成之焦炭量小於重餾分之焦炭 ' 1而促進催化劑循環。改良C/0比率且促進重館分之催化轉化。【先前技術】 f 熟習此項技術者知曉輕餾分之催化裂化係由一般比重餾分之催化裂化嚴格的條件促進。術語"更嚴格條件"意謂較高裂化溫度、較高催化劑循環及較長滯留時間。舉例而έ ’為有效地裂化汽油（其被視為輕餾分），關於溫度（通常為530-700。〇、C/0(通常為10_30)及滯留時間（1 s-30 s)之條件比彼等用於裂化重餾分之條件嚴格得多。使不同油餾分在不同嚴格度條件下裂化之兩個獨立反應〇 d的，组合為热習此項技術者&知。因此，可能在主要反應器中裂化產生大量汽油及LPG之重烴餾分，且在專用第二 &應H中使所產生之含有特別在㈣產生中具反應性之長鏈C 5 +烯烴的汽油部分再裂化。亦可能在專用第二反應器中使先前已經寡聚以形成長鍵烯烴之一部分C4-C5烯烴再裂化。若再循環至第二反應器中之餾分係由來自c4_c5餾分之特別反應性寡聚物構成，則該再裂化可在不有損於總汽油產率下大幅增加丙烯之產生。 131895.doc 200911975 熟習此項技術者亦知曉，以具有形成選擇性之特定彿石 (諸如ZSM-5)補充Fcc催化劑（基本上由促進催化裂化以產生汽油之USY沸石構成）可促進產生丙烯。在豎管出口處’將氣體排出物自催化劑顆粒分離以終止催化反應且自反應器快速排空氣體排出物。亦可能儘可能地限制由於排出物延時曝露於接近豐管出口處所處溫度之溫度水平而產生的排出物之熱降解。為此目的’已研發氣-固分離技術來促進快速分離^管出口處之氣體排出物與催化劑。因此，歐洲專利m 017 762描述包含一組以交替方式環繞g管排列之分離腔室及汽提腔室之氣·固分離系統。此系統可同時進行以下操作： •於分離腔室中分離氣體與顆粒； •經由官線向汽提器中引人於分離腔室中分離之大部分催化劑，從而使夹帶之烴減至最少； •使來自分離腔室之氣體通過汽提腔室中，汽提腔室可將乳體與催化劑顆粒完全分離，且將該氣體與源自汽提器之排出物混合； •將源自汽提器及汽提腔室之所有氣體排出物快速排空至反應益旋渴分離器中以在離開反應器之前最後分離。亦可肊驟冷反應排出物以限制來自FCC反應區之排出物之熱降解。因此’專利US-A-5 089 235、US-A-5 087 7 US-A-5 043 058及WO-91/14752描述可降低反應區下 131895.doc •12- 200911975 游溫度且因此限制熱裂化反應之裝置。因此，在氣體-顆粒分離之下游，可能注射在與來自反應區之排出物接觸時 π化且因此使介質冷卻之烴。可使得此注射進入來自分離器之氣體出口’或進入反應器之稀釋相中。【發明内容】可將本發明描述為包含下列各物之反應區： •進行重饋料之催化裂化之主要反應器（1〇〇)，其包含稀釋相區（110) ’該稀釋相區（110)含有a)藉由快速分離系統（20，30)，隨後藉由第二分離系統（7〇)終止之主要豎官（1 〇)的上部；b)用於注射位於快速分離系統與第二分離系統之間的驟冷流體（1〇5)之裝置；为用於注射位於稀釋相（11〇)上部之沖洗流體（1〇4)之裝置，該主要反應器（100)之下部另外包含使催化劑經汽提之緻密相區（12 1); •一或多個在比主要豎管（10)高之嚴格度下操作且進行〇輕餾分的催化裂化之額外豎管（210)，該等額外豎管 (210)係與主要豎管（1〇)平行操作；將來自額外登管（21〇)之氣態及固態排出物傳送至主要反應器（100)之稀釋區（110)。 " 術語來自額外一或多個豎管之，，氣態及固態排出物”意謂由來自額外一或多個豎管之氣態反應排出物及於額外一或多個豎管中循環之催化劑所形成之組。在本發明之較佳變型中，初始將來自額外一或多個豐管 (210)之排出物分離為含有反應排出物（221)之主要氣相及 13 lS95.doc -13- 200911975 含有裂化催化劑（222)之主要固相，將氣相傳送至主要反應器（100)之稀釋相區（11〇)，且將固相傳送至主要反應器 (100)之緻密相區（121)。在本發明之較佳變型中，用於控制來自反應區之排出物服度之大部分（亦即超過7〇%且較佳地超過8〇%)驟冷流體係由與來自額外一或多個豎管之排出物（221)一起注射之驟冷流體（23 0)構成。, the worker then recycles the % cracked fraction into the standpipe that absorbs waste heat during vaporization: a possible solution to meet the heat balance. Finally, placing an exchanger (generally referred to as a catalytic cooler in the art) is placed in the regeneration zone to absorb some of the residual heat, for example, by generating hot gas and cooling the catalyst. By using one or more of the above techniques, it is possible to convert the catalytic cracking of the Conradson carbon heavy fraction in 15% by weight, preferably less than 1% by weight, by catalytic cracking to produce between dry gas and conversion. Emissions within the residue range. The following fractions are classified as effluents and are usually defined by their composition or their point of change: • Dry and acid gases (mainly: H2, h2S, ci, C2); • Liquefied petroleum gas containing C3-C4 molecules 3) Gasoline with heavier hydrocarbons having a boiling point of less than 220 C (standard eut p〇int); • Standard 220-360. . Diesel in the boiling range, which is highly aromatic and is therefore referred to as LCO (light cycle oil); • Conversion residue having a boiling point in excess of 36 〇t:2. It may be noted that some of their fractions are recycled to cause their catalytic cracking again. It is also possible to recycle fractions produced directly by the FCC or fractions produced by the FCC but subjected to post-ik conversion. For example, it is possible to crack light gasoline from the FCC having a boiling range and rich in olefins to facilitate the production of propylene. 131895.doc 200911975 This self-evaporation separation is rich in c4_C5 points, said! The fraction of the π knife is used to condense the olefin and then crack the oligomer. It is also possible to try to recover the LCO, so that when the gas is used as a fraction, it will be plutonized and then cracked, and then the fraction will be cracked. On the other hand, it will be more favorable for the catalytic modification of catalytic cracking. Evening combinations are possible. Also, the soil of the J J month and the FCC_ injection of the light fraction from the other side to convert it catalytically! ^ This, for example, may try to catalyze petrochemical naphtha. It is also possible to try to catalyze the cracking of light hydrocarbons derived from the source of the ancestors or the source of the animal. The feedstock consists of all the vegetable oils and animals mainly containing gan', from a female glycerol glycerin and fatty acid or ester. Fat composition, its, τ heart such as fat chain contains 6 to 25 carbon atoms in ° such oil can be African oil, in the Nag, 丄 seed m mountain solid oil, coconut oil, sesame oil or cotton metaplasia , from linseed oil and mustard oil, s age / from humic oil and from any oil produced, for example, to sundial or rapeseed or by genetic modification or hybridization. Also used are frying oils, various animal oils (such as fish oil, animal fat or slabs, etc., which have no or no aromatics-containing sulfur and nitrogen-containing compounds, and also such feeds, vegetable oils or Animal fats are used in the present invention, (1) the initial pretreatment or pre-refining steps using suitable treatments to remove various contaminants. Let 3 be defined as having at least 80% by weight of a boiling point of less than 340T: Molecular and including the first step of the vegetable oil and animal fat light fraction catalytic cracking can significantly change the yield structure of the heavy fraction FCC: first transfer selectivity. For example, by the subsequent cracking 131895.doc 200911975 C4-C5 The fraction is pooled to convert into the rC4_C5 fraction to produce an olefin-rich C3 fraction; • secondly, the heat of reaction of the injected lighthouse is changed by the heat balance of the endothermic unit, which is smaller than the heavy fraction due to the amount of coke formed. Coke '1 promotes catalyst circulation. Improves C/0 ratio and promotes catalytic conversion of heavy sites. [Prior Art] f Those skilled in the art are aware that the catalytic cracking of light fractions is generally The strict conditions of catalytic cracking of heavy fractions are promoted. The term "stricter conditions" means higher cracking temperatures, higher catalyst cycles and longer residence times. For example, έ 'is effectively cracked gasoline (which is considered light Fractions), conditions for temperature (usually 530-700. 〇, C/0 (usually 10-30) and residence time (1 s-30 s) are much stricter than those used to crack heavy fractions. The two separate reactions 〇d of the oil fraction cracking under different stringency conditions are combined and known to those skilled in the art. Therefore, it is possible to crack a large amount of gasoline and heavy hydrocarbon fractions of LPG in the main reactor, and The resulting portion of the gasoline containing the long chain C5+ olefins which are particularly reactive in (4) production is re-cracked in a dedicated second & H. It is also possible to have previously oligomerized in a dedicated second reactor. Forming a portion of the long-chain olefin, the C4-C5 olefin is re-cracked. If the fraction recycled to the second reactor is composed of a particularly reactive oligomer from the c4_c5 fraction, the re-cracking can be without detrimental to the total gasoline. Large yield Addition of propylene. 131895.doc 200911975 It is also known to those skilled in the art to supplement the Fcc catalyst with a specific fossil having a selective selectivity (such as ZSM-5) (consisting essentially of USY zeolite which promotes catalytic cracking to produce gasoline) Promotes the production of propylene. At the outlet of the riser, the gas effluent is separated from the catalyst particles to terminate the catalytic reaction and the effluent is quickly vented from the reactor. It is also possible to limit the exposure of the effluent to the outlet close to the main pipe as much as possible. The thermal degradation of the effluent resulting from the temperature level of the temperature at the location. For this purpose, a gas-solid separation technique has been developed to facilitate rapid separation of the gas effluent and catalyst at the outlet of the tube. Thus, European Patent No. 017 762 describes a gas-solid separation system comprising a plurality of separation chambers and stripping chambers arranged in an alternating manner around a g-tube. The system can simultaneously perform the following operations: • Separation of gases and particles in the separation chamber; • Exposure of most of the catalyst separated in the separation chamber to the stripper via the official line to minimize entrained hydrocarbons • passing gas from the separation chamber through the stripping chamber, which separates the emulsion from the catalyst particles and mixes the gas with the effluent from the stripper; All gas effluent from the stripper and stripping chamber is quickly vented to the reaction-spinner separator for final separation prior to exiting the reactor. The reaction effluent can also be quenched to limit thermal degradation of the effluent from the FCC reaction zone. Therefore, the patents US-A-5 089 235, US-A-5 087 7 US-A-5 043 058 and WO-91/14752 describe the reduction of the temperature under the reaction zone 131895.doc •12-200911975 and thus limit the heat A device for cracking reaction. Thus, downstream of the gas-particle separation, it is possible to inject hydrocarbons that are π-phased and thus cool the medium upon contact with the effluent from the reaction zone. This injection can be caused to enter the gas outlet from the separator or into the dilution phase of the reactor. SUMMARY OF THE INVENTION The invention may be described as a reaction zone comprising: • a primary reactor (1〇〇) for catalytic cracking of a heavy feed comprising a dilution phase zone (110) 'the dilution phase zone ( 110) comprising a) an upper part of a main vertical (1 〇) terminated by a rapid separation system (20, 30) followed by a second separation system (7〇); b) for injection in a rapid separation system and a device for quenching fluid (1〇5) between two separation systems; a device for injecting a flushing fluid (1〇4) located in the upper portion of the diluted phase (11〇), the lower portion of the main reactor (100) Including a dense phase zone (12 1) for stripping the catalyst; • one or more additional risers (210) operating at a higher stringency than the main riser (10) and undergoing catalytic cracking of the bismuth light fraction, The additional standpipes (210) operate in parallel with the main standpipe (1 inch); the gaseous and solid effluent from the additional pipe (21 inches) is delivered to the dilution zone (110) of the main reactor (100). "terminology from additional one or more standpipes, gaseous and solid effluent" means a catalyst that is circulated from a gaseous reaction effluent from one or more standpipes and circulated in one or more additional risers. In a preferred variant of the invention, the effluent from the additional one or more headers (210) is initially separated into a main gas phase containing the reaction effluent (221) and 13 lS95.doc -13- 200911975 Contains the main solid phase of the cracking catalyst (222), transports the gas phase to the dilute phase zone (11〇) of the main reactor (100), and transports the solid phase to the dense phase zone of the main reactor (100) (121 In a preferred variant of the invention, the quenching flow system for controlling the majority of the effluent from the reaction zone (i.e., more than 7% and preferably more than 8%) is derived from Or the quenching fluid (23 0) of the plurality of riser discharges (221) is injected together.

在本發明之另一較佳變型中，在主要反應器（1〇〇)之稀釋相區（110)中保持特定流動之大部分（亦即超過7〇%，較 it·超過80%)沖洗流體係由來自額外一或多個豎管之排出物 (221)構成。其意謂在本發明之反應區中，該等特徵使得主要反應器 (1 〇〇)之稀釋相區（11 0)的溫度（T5)—般在49〇t至52CTC範圍内，且自將重饋料引入主要賢管（10)底部至反應排出物自主要反應器（1 〇〇)排出之出口所量測之試劑滯留時間一般小於1 0秒。本發明亦可描述為使用根據本發明之反應區產生丙烯之 ^法，其中主要豎管之饋料為重餾分，且至少一個額外豎官中之饋料為含有至少30重量％烯烴之輕餾分，其中至少 8〇%分子具有小於34〇t之滞點。本發明之變型中’至少一個額外豎管中之饋 ^ ^ Φ ±. Λ. 產生且含有至少3〇%烯烴之輕汽油（C5_15(rc)。在本發明之另一變型巾，至少一個額外豎管中之饋料為、’、自主要豎管之C4或C5輕烯烴產生之募聚汽油。 131895.doc -14- 200911975 最後，在本發明之另一變型巾，至少、—個額外登管中之饋料亦可為植物油或動物脂肪或植物油與動物脂肪之任何混合物。本發明之反應區與主要反應器及額外一或多個豎管中之垂二下向流相容。通常在此情況下，以”滴管”替換術語丘官"。然而，為保持術語簡單，將術語"豐管”用於流之特定情況。 =地’分㈣"緻密區⑴料，，稀釋區（121)"替換表述稀釋相區（110)'，及”緻密相區（121)，，。本發明之反應區之一流體動力學結果為使用來自額外— =個豐管之排出物作為來自主要反應器之排出物贈體變得有可能。因此，將大邱八趙細。/… 將大#刀（亦即超過70%且較佳地超匕/。)來自主要反應器之驟冷流體與來自額登管之排出物⑽）-起注射。在特定情況下，亦可能有驟冷流體⑽)與來自額外—或多個豎管之❹物In another preferred variant of the invention, a substantial portion of the specific flow (i.e., more than 7〇%, more than 80%) is maintained in the dilute phase zone (110) of the main reactor (1〇〇). The flow system consists of an effluent (221) from an additional one or more standpipes. It means that in the reaction zone of the present invention, the characteristics such that the temperature (T5) of the diluted phase zone (11 0) of the main reactor (1 —) is generally in the range of 49 〇t to 52 CTC, and The reagent retention time measured by the feed of the heavy feed to the bottom of the main sump (10) to the discharge of the reaction effluent from the main reactor (1 〇〇) is generally less than 10 seconds. The invention may also be described as a process for producing propylene using a reaction zone according to the invention, wherein the feed to the main standpipe is a heavy fraction and the feed in at least one additional stand is a light fraction containing at least 30% by weight of olefins, At least 8% of the molecules have a stagnation point of less than 34 〇t. In a variant of the invention 'feeding in at least one additional standpipe ^ Φ ±. 轻. Light gasoline (C5_15(rc)) which produces and contains at least 3 % olefin. In another variant of the invention, at least one additional The feedstock in the riser is, ', the polycondensed gasoline produced from the C4 or C5 light olefins of the main standpipe. 131895.doc -14- 200911975 Finally, in another variant of the invention, at least one extra The feed in the tube may also be vegetable oil or animal fat or any mixture of vegetable oil and animal fat. The reaction zone of the present invention is compatible with the main reactor and the downward flow in the additional one or more standpipes. In this case, replace the term "qiuguan" with "dropper". However, in order to keep the term simple, the term "fengguan" is used for the specific case of flow. = ground 'minutes (four) " dense area (1) material, diluted Zone (121) "Replacement of Diluted Phase Zone (110)', and "Dense Phase Zone (121)," One of the reaction zones of the present invention results in fluid dynamics using effluent from additional - = abundance As the effluent from the main reactor becomes available Yes, therefore, Daegu Ba Zhao is fine./... The big #刀 (that is, more than 70% and preferably more than 。). The quenching fluid from the main reactor and the effluent from the hedging pipe (10)) - Inject. In certain cases, there may also be quenching fluids (10) and stolen goods from additional or multiple risers.

U 射。 ~ ’土 ::明之反應區之另一流體動力學結果為可能省卻主要反應器的稀釋相中之沖洗流體（〗〇4)。屮：Γ之一目標為藉由使用—般快速分離系統對所有排出物產生較短滞留時間而使得同時控制來自主要及額外-或多個豎管(210)之排出物的滞留時間。本發明之目標亦為藉由在受控溫度條件下 =應器⑽）之稀釋相⑽）而改良主要反應器⑽ 131895.doc 15 200911975 最後，本發明之另一優勢在於以下事實：將來自主要豎管（ίο)之氣體排出物更有效地限制於快速分離器中且使其無法自位於該快速分離器周圍之稀釋區（110)逸出，其構成確保更佳控制快速分離系統中此等排出物之滯留時間。【實施方式】為以下描述之明確性，將術語"反應區"用於由用以催化裂化重烴餾分之主要賢管，用以在比裂化重餾分之條件更嚴格之條件下裂化輕烴餾分的額外一或多個豎管及位於主要豎管末端且由豎管總成共用之快速分離系統所構成的總成。術語"反應器，，，或有時為避免意義不明而為，，主要反應器’’表示由主要豎管上部，安裝在主要豎管出口處之快速分離系統，與快速分離系統連接之旋渦分離器及位於反應器下部之緻密汽提床（亦稱作汽提器）所形成的總成。以此方式界定之反應器含於腔室（100)中，因此該腔室 (100)包含表示為（110)之稀釋區及表示為（121)之緻密區或八提态。為簡單起見，以界定反應器之腔室（100)來鑑別反應器。因此，可將本發明之反應區定義為主要反應器（100)與額外一或多個豎管（210)之組合。因此，本發明描述由可進行重烴餾分（後文稱作重饋料）之催化裂化之主要登管^…，及可裂化輕餾分之一或多個額外豎官（2 1 〇)構成的反應區，此等輕餾分可能為任何來源之石油腦，可預先經寡聚之部分不飽和烴（諸如以或以烯 I31895.doc -16- 200911975 烴）或最終植物油或動物脂肪。 a月反應區之特徵為以下事實：分離源自主要豎管及、或夕個豎管之氣-固排出物係使用一般快速分離系統來進行。 y' 將此一般快速分離系統安裝於裂化重饋料之主要豎管 0〇)的出口處。江圖—展示本發明反應區之一實施例。主要豎管（10)終止於包含沖洗裝置（1G4)及用於驟冷排出物之裝置（1〇5)之快速分離系統。、為使此快速分離器之功能最佳化，有必要使來自汽提器 (12〇)且穿過連接汽提腔室（3G)與主要反應II (1GG)的稀釋區 (110)之開口（26)之氣體具有足夠流動速率。經由此等開口（26)升起之氣流使得源自豎管（1〇)之烴含於汽提腔室（3〇)中。更確切地，其可防止來自豎管⑽之排出^滲透至稀釋區（11〇)中，稀釋區（11〇)為排出物可以 Ο ，循環速率長期停留且由於該稀釋n(iiG)中所盛行之相對咼溫而熱降解之區。匕外由於經由反應器之稀釋區（110)之壁造成的埶損 .耗，可致使與高速率流動區(2。、3。、4。、5。、二知 70)相比，該區（11〇)之壁顯著冷卻。此冷部可冷卻高達—百度，且可引起在所論及之冷壁、更確切地在氣體循環速率較低之區中之冷壁上形成焦炭。為避免此現象(其可導致單元堵塞)，可能將氣態流體注射至反應器（1 04)之頂部，其將不斷地再生區（1 1 〇)中之氣體 131895.doc 200911975 容積且因此避免可熱降解之烴積聚。注射至反應器⑽)頂部之氣體(稱作沖洗氣體)一般為蒸汽，但其亦可為在稀釋區（110)所處之條件下（亦即通常 400-5 5 0°C)不熱降解之另一種輕氣體。本發明提供可以源自額外一或多個豎管（21〇)(其中進行輕餾分之高度嚴格裂化）之氣態排出物替換大部分或甚至所有沖洗氣體（104)之解決方案。本文之剩餘部分描述主要豎管（丨〇)及含於主要反應器 (1 00)之稀釋區（11 〇)中之快速分離系統。來自再生區（未於圖1中展示）之再生催化劑⑴係於豐管 (1〇)之下端引入。藉由無法在豎管⑽底部之溫度及壓力條件下濃縮之充氣氣體使催化劑保持流體化狀態。可藉由主射(11)基本上氣態之流體(蒸汽，輕餾分)使其加速以使與重饋料之接觸最佳化。使用可使液態之該饋料霧化成精細液滴之構件〇 2)將重饋料引入反應區中以與催化劑接觸。可能使用安置於重饋料（12)之注射點下游（反應流體的流動方向)之構件(13，14)來引入基本上液態之流冑。在汽化時’此液體⑴）、（14)將降低反應介質之溫度，使沿登管 (1 〇)之溫度分布最佳化。在裂化反應效應下，確立可㈣管⑽之全長上傳輸催化劑之軸速度概況。在豎f (10)之出口處，於藉由與安置於豎管（1 Μ的上端周圍之-或多個汽提腔室(3 〇)交替排列一或多個分離腔室 131895.doc -18- 200911975 (20)而構成之快速分離裝置（2〇 ’ 30)中將氣態烴與催化劑分離。源自豎管（1 〇)之氣-固混合物經由入口部分（2 1)滲透至分離腔室（20)中，且在離心力效應下，固體顆粒向分離腔室 (20)之外壁遷移，從而使氣體釋放。固體顆粒經由專用於催化劑（22)且接合至緻密汽提床（12 1)之向下定向出口離開分離腔室（20)。氣體繞偏導(2 3 )叙轉且經由使得與相鄰汽提腔室（3 〇) ^ 連通之開口（25)向外離開分離腔室（20)。分離腔室（20)之入口部分（2 1)中之氣-固混合物速度一般在10 m/s至40 m/s之範圍内，且較佳地在15爪“至^爪仏之範圍内。分離腔室（20)之出口部分（22)中之催化劑的表面流動速率般在1 0 kg/s_m至300 kg/s.m2之範圍内，且較佳地在 5〇 kg/s.m2至200 kg/s.m2之範圍内，以限制不良地夾帶具 r , 有催化劑之烴蒸氣。、二由開口（25)之氣體速度一般在10 m/s至40 m/s之範圍内，較佳地在1 5 m/s至3 0 m/s之範圍内。將通入汽提腔室(30)中之氣體與來自汽提器(121)的經由 T於汽提腔室（3〇)下部之開口（26)渗透至汽提腔室（3〇)中之軋體混合。應注意，來自汽提器(121)之氣體僅可經由開口 (，）排工。接著’發現經由出口（22)以催化劑之逆流形式、\之源自提盗之任何少量氣體均在汽提腔室（3〇)中。由位於'飞提腔室（3〇)上部之共同開口（29)排空來自汽 I31895.doc -19- 200911975 提腔室（30)之氣體，該共同開口（29)係經由垂直管線（4〇， 6〇) ’接著經由水平管線（73)與一般由漩渦分離器（7〇)構成之第一分離糸統連通。有可能將機械構件（50)置於垂直管線（40，60)上，該構件可消減豎管（1〇)頂部與豎管（1〇)下部之間的差異性膨服。U shot. Another hydrodynamic result of the ~' soil:ming reaction zone is that it is possible to dispense with the flushing fluid in the dilute phase of the main reactor ("4>). One of the goals is to achieve a shorter residence time for all emissions by using a fast separation system to simultaneously control the residence time of the effluent from the primary and additional-or multiple risers (210). The object of the invention is also to improve the main reactor (10) by means of a dilute phase (10) of the reactor (10) under controlled temperature conditions. 131895.doc 15 200911975 Finally, another advantage of the invention lies in the fact that it will come from the main The gas effluent of the standpipe is more effectively confined in the fast separator and is rendered incapable of escaping from the dilution zone (110) located around the fast separator, which constitutes a better control in the fast separation system. The residence time of the effluent. [Embodiment] For the clarity of the following description, the term "reaction zone" is used for the main sage used to catalytically crack heavy hydrocarbon fractions for cracking lighter under conditions more severe than cracking heavy fractions. An additional one or more risers of the hydrocarbon fraction and an assembly of rapid separation systems located at the end of the main riser and shared by the riser assembly. The term "reactor,, or sometimes to avoid meaning, the main reactor '' denotes a vortex connected from the upper part of the main riser, to the quick separation system installed at the exit of the main standpipe, to the fast separation system An assembly formed by a separator and a dense stripping bed (also referred to as a stripper) located at the lower portion of the reactor. The reactor defined in this manner is contained in the chamber (100), and thus the chamber (100) contains a dilution zone denoted as (110) and a dense zone or an eight-lift state denoted as (121). For simplicity, the reactor is identified by a chamber (100) defining the reactor. Thus, the reaction zone of the present invention can be defined as a combination of a primary reactor (100) and an additional one or more risers (210). Accordingly, the present invention is described in terms of a primary tube that can perform catalytic cracking of a heavy hydrocarbon fraction (hereinafter referred to as a heavy feed), and one or more additional vertical members (2 1 〇) of a crackable light fraction. In the reaction zone, such light fractions may be petroleum brains of any origin, partially oligomerized by oligomerization (such as hydrocarbons with or with an olefin I31895.doc -16-200911975) or final vegetable oil or animal fat. The a month reaction zone is characterized by the fact that the separation of the gas-solid effluent from the main riser and/or the riser is carried out using a generally rapid separation system. y' Install this general rapid separation system at the outlet of the main riser 0〇) of the cracking heavy feed. Jiangtu - shows an embodiment of the reaction zone of the present invention. The main standpipe (10) terminates in a rapid separation system comprising a flushing device (1G4) and means for quenching the effluent (1〇5). In order to optimize the function of the fast separator, it is necessary to open the opening from the stripper (12〇) and through the dilution zone (110) connecting the stripping chamber (3G) with the main reaction II (1GG). The gas of (26) has a sufficient flow rate. The gas stream raised by the opening (26) is such that hydrocarbons originating from the standpipe (1〇) are contained in the stripping chamber (3〇). Rather, it prevents the discharge from the standpipe (10) from penetrating into the dilution zone (11〇), the dilution zone (11〇) is effluent, the cycle rate stays for a long time and due to the dilution n(iiG) The prevailing area of relatively hot and thermally degraded. The area can be caused by the damage caused by the wall of the dilution zone (110) of the reactor, which can be compared with the high rate flow zone (2, 3, 4, 5, 2, 70). The wall of (11〇) is significantly cooled. This cold portion can be cooled up to - Baidu and can cause coke formation on the cold wall in the zone in question, more precisely in the zone where the gas circulation rate is lower. To avoid this phenomenon, which can lead to blockage of the unit, it is possible to inject a gaseous fluid to the top of the reactor (104), which will continuously regenerate the volume of the gas in the zone (1 1 〇) 131895.doc 200911975 and thus avoid Thermally degraded hydrocarbons accumulate. The gas injected to the top of the reactor (10) is generally referred to as steam, but it may also be thermally degraded under the conditions of the dilution zone (110) (ie typically 400-5 50 °C). Another light gas. The present invention provides a solution that can replace most or even all of the flushing gas (104) from a gaseous effluent that can be derived from one or more additional risers (21 〇) in which the lightly severe cracking of the light ends is carried out. The remainder of this document describes the main standpipe (丨〇) and the fast separation system contained in the dilution zone (11 〇) of the main reactor (100). The regenerated catalyst (1) from the regeneration zone (not shown in Figure 1) was introduced at the lower end of the header (1〇). The catalyst is maintained in a fluidized state by an inflating gas that cannot be concentrated under the conditions of temperature and pressure at the bottom of the standpipe (10). The contact with the heavy feed can be optimized by the primary (11) substantially gaseous fluid (steam, light fraction). A member that atomizes the liquid feed into fine droplets is used. 2) A heavy feed is introduced into the reaction zone to contact the catalyst. It is possible to use a member (13, 14) disposed downstream of the injection point of the heavy feed (12) (the flow direction of the reaction fluid) to introduce a substantially liquid flow. At the time of vaporization, the liquids (1) and (14) will lower the temperature of the reaction medium and optimize the temperature distribution along the tube (1 〇). Under the effect of the cracking reaction, an overview of the axial velocity of the transporting catalyst over the entire length of the (iv) tube (10) is established. At the exit of the vertical f (10), one or more separation chambers 131895.doc are alternately arranged by being disposed between the upper end of the vertical tube (1 Μ or the plurality of stripping chambers (3 〇) 18- 200911975 (20) The rapid separation device (2〇' 30) is constructed to separate gaseous hydrocarbons from the catalyst. The gas-solid mixture from the standpipe (1 〇) permeates into the separation chamber via the inlet portion (2 1) In the chamber (20), and under the effect of centrifugal force, the solid particles migrate toward the outer wall of the separation chamber (20) to release the gas. The solid particles are dedicated to the catalyst (22) and joined to the dense stripping bed (12 1) The downwardly directed outlet exits the separation chamber (20). The gas is deflected around the deflector (23) and exits the separation chamber outwardly via an opening (25) that communicates with the adjacent stripping chamber (3?) (20) The velocity of the gas-solid mixture in the inlet portion (21) of the separation chamber (20) is generally in the range of 10 m/s to 40 m/s, and preferably in the 15 claws "to the claws" Within the range of 仏. The surface flow rate of the catalyst in the outlet portion (22) of the separation chamber (20) is in the range of 10 kg/s_m to 300 kg/s.m2, and Preferably, the range is from 5 〇kg/s.m2 to 200 kg/s.m2 to limit the poor entrainment of the hydrocarbon vapor with the catalyst, and the gas velocity of the opening (25) is generally 10 m/ s in the range of 40 m/s, preferably in the range of 15 m/s to 30 m/s. The gas introduced into the stripping chamber (30) and the stripper (121) The mixture is infiltrated into the stripping chamber (3〇) via the opening (26) in the lower portion of the stripping chamber (3〇). It should be noted that the gas from the stripper (121) can only pass through the opening. (,) Discharge. Then 'discover any small amount of gas from the outlet (22) in the form of countercurrent flow of the catalyst, which is from the stolen chamber. It is located in the stripping chamber (3〇). 3〇) The common opening (29) in the upper part is emptied from the gas from the steam chamber I31895.doc -19- 200911975, and the common opening (29) is via the vertical line (4〇, 6〇)' The horizontal line (73) is in communication with a first separation system generally comprised of a vortex separator (7 〇). It is possible to place the mechanical member (50) on a vertical line (40, 60) which can attenuate the riser ( 1〇) Standpipe portion (1〇) differential expansion between the lower clothing.

進入旋渦分離器（70)之氣體中的固體濃度一般比豎管 (10)上部中之濃度小約4倍。接著，將通過漩渦分離器（7〇)後經汽提之排出物經由管 Ί (71 8〇)自反應器排空且使其經由一般置放於該反廯考 (1〇〇)頂部之管線（101)離開主要反應器（1〇〇)。使用該裝置，一般可能在少於5秒内排空烴排出物，此時間對應於豎管⑽之出口 (21)與反應器(1〇〇)之出口。⑴) 之間所消耗時段。總體而言，自引入主要登管⑽底部至離開反應器（_之反應流體滯留時間—般少於1〇秒。 :限制排出物在登管⑽出口處之溫度較高時熱降解， /使㈣於引入該流體⑽），使其快速汽化，從而流體溫度顯著下降之構件將基本上液態之流體（105)例如 ^直S線（40)處注射至出口（29)之下游。顯然， (73)中。至官線（60)或管線亦可將此冷卻流體（1 05)注射注射之區中自主要裂化此冷卻流體（亦稱作驟冷流體）一般為可在所盛行之條件下汽化之烴。此流體可為(例如)源之LCO(輕循環油）。 13I895.doc •20* 200911975 經由出口（22)自分離腔室（20)排空之催化劑流入用作緻密流體化床（121)之汽提區中，該汽提區構成反應器（100) 之下部，在該汽提區中’在各種水平（1 20，1 30)處引入之蒸汽可使催化劑流體化且促進吸附於該催化劑上之烴的解 - 吸附。 • 促進下降催化劑與上升蒸氣之間之逆流接觸的結構化或内部裝填元件（140)可在汽提區（121)之各點處經整合。汽提蒸氣及解吸附之烴離開汽提區（121),向反應器（1〇〇)之稀釋區（110)行進。可將經提之催化劑經由用以接合再生區（未於圖丨中展示）之管線（103)自汽提區（121)排空。接著，所有氣體（汽提蒸氣（102)及（12〇)及解吸附之烴）經由開口（26)通入汽提腔室（3〇)中，其中維持一般在丨1^/8至5 m/s|巳圍内，較佳地15至4 m/s範圍内之最佳化上升速度。應注忍，此速度影響汽提腔室（3 〇)之效率，因為該汽提腔 Ό 至（〇)之内邛可經由開口（25)含有源自分離腔室（20)之氣 βΑ 體0 2具有伸長管狀形狀之額外豎管（21〇)大體上平行於主要=管（1G)安置以進行輕館分之催化轉化。圖丨顯示單—額外=官，但本發明涵蓋將複數個額外豎管大體上平行於主要登管(10)安置之情況，此等額外豎管各自能夠輕餾分。 u π向額外I管⑽）中饋人源自與用以使主要登管㈣中循衣之催化劑再生之再生區相同的再生區（未於圖2中展示）之 131895.doc •21 · 200911975 催化劑流（201)。可引入基本上氣態之流體（211)以調節豎管（21〇)入口處之催化劑之流體化流。將待裂化之輕館分（212)經由促饋料（2丨2)與催化劑之間均句接觸之構件引入登管（2if) 中。此等用於引人待裂化之輕館分（212)之構件可為與用以將重饋料(12)引入主要豎管⑽中之彼等構件相同之類型。、視情況，可沿額外g管（210)之長度將其他輕館分（未於圖1中展示）引人_分引人（212)下游以使其亦與催化劑反應。基本上由於較少焦炭沈積，故輕餾分之催化劑失活較低，且可能（例如）將具有較高反應性之饋料注射至第一次注射之輕饋料（21 2)下游。在展示於圖1中之本發明較佳變型中，在豎管（21〇)出口處，將初始氣-固分離器（220)安裝於額外豎管（21〇)之出口處。在圖1中，此氣-固分離系統以漩渦分離器（22〇)為代表，但亦可使用任何其他氣-固分離系統，例如可設計位於豎管（210)上端之分離裝置，諸如三通管，且其在本發明反應區之範_内。此分離器（220) —般可覆蓋至少70%之固體顆粒，可經由分離器之出口（222)將該等固體顆粒再引入主要反應器中，該分離器之出口接近主要反應器（100)的汽提區（121)之流體化床水平。 131895.doc -22- 200911975 術語”接近”意謂主要反應器（100)之汽提區（121)的緻密床水平以上或以下約5公尺，較佳約3公尺之距離。於稀釋相（110)之任何水平處’將經清潔之排出物（221) 再引入主要反應器（100)之該稀釋相（11 〇)中，但較佳地引入該區的上部。由於額外豎管（210)之溫度一般大體上高於主要豎管（1〇) 之溫度’故注射驟冷流體（230)可限制排出物（221)之温 fThe concentration of solids in the gas entering the vortex separator (70) is generally about 4 times less than the concentration in the upper portion of the riser (10). Next, the stripped effluent passing through the vortex separator (7 Torr) is evacuated from the reactor via a tube (71 8 Torr) and placed through the top of the counter (1 〇〇). Line (101) leaves the main reactor (1〇〇). With this device, it is generally possible to evacuate the hydrocarbon effluent in less than 5 seconds, which corresponds to the outlet of the riser (10) and the outlet of the reactor (1). (1)) The period of time consumed between. In general, from the bottom of the main inlet pipe (10) to the exit of the reactor (the reaction time of the reaction fluid is less than 1 sec.): limiting the thermal degradation of the effluent at the higher temperature at the outlet of the pipe (10), / (d) by introducing the fluid (10)) to rapidly vaporize, whereby the member having a substantially reduced fluid temperature injects a substantially liquid fluid (105), for example, at a straight line S (40) downstream of the outlet (29). Obviously, (73). To the official line (60) or pipeline, this cooling fluid (10) can also be injected into the injection zone from the main cracking. This cooling fluid (also known as quenching fluid) is generally a hydrocarbon that can be vaporized under prevailing conditions. This fluid can be, for example, a source of LCO (light cycle oil). 13I895.doc • 20* 200911975 Catalyst vented from the separation chamber (20) via the outlet (22) flows into a stripping zone serving as a dense fluidized bed (121), which forms the reactor (100) In the lower portion, the steam introduced at various levels (1 20, 130) in the stripping zone fluidizes the catalyst and promotes the desorption-adsorption of hydrocarbons adsorbed on the catalyst. • The structured or internal packing element (140) that promotes countercurrent contact between the descending catalyst and the rising vapor can be integrated at various points in the stripping zone (121). The stripped vapor and desorbed hydrocarbon exit the stripping zone (121) and travel to the dilution zone (110) of the reactor (1〇〇). The catalyst can be vented from the stripping zone (121) via a line (103) for engaging a regeneration zone (not shown). Next, all gases (stripping vapor (102) and (12〇) and desorbed hydrocarbons) are passed through the opening (26) into the stripping chamber (3〇), which is maintained generally at 丨1^/8 to 5 Within m/s|巳, preferably the optimum rate of rise in the range of 15 to 4 m/s. It should be noted that this speed affects the efficiency of the stripping chamber (3 ,) because the stripping chamber Ό to (〇) can contain the gas β Α derived from the separation chamber (20) via the opening (25). An additional riser (21〇) having an elongated tubular shape is placed substantially parallel to the main = tube (1G) for catalytic conversion of the light column. The figure shows a single-external = official, but the present invention covers the case where a plurality of additional standpipes are placed substantially parallel to the main pipe (10), each of which can be lightly distillate. u π is fed to the additional I tube (10) from the same regeneration zone as the regeneration zone used to regenerate the catalyst in the main tube (4) (not shown in Figure 2). 131895.doc • 21 · 200911975 Catalyst stream (201). A substantially gaseous fluid (211) can be introduced to regulate the fluidization of the catalyst at the inlet of the riser (21〇). The member to be cracked (212) is introduced into the tube (2if) via a member that facilitates the contact between the catalyst (2丨2) and the catalyst. The components of the light house segment (212) for inducing cracking may be of the same type as the members used to introduce the heavy feed (12) into the main riser (10). Depending on the situation, other light pavilions (not shown in Figure 1) may be introduced along the length of the additional g-tube (210) to direct (212) downstream to also react with the catalyst. The catalyst of the light ends is less deactivated, essentially due to less coke deposition, and it is possible, for example, to inject a feed having higher reactivity downstream of the first injected light feed (21 2). In a preferred variant of the invention shown in Figure 1, the initial gas-solid separator (220) is installed at the outlet of the riser (21〇) at the outlet of the additional riser (21〇). In Fig. 1, the gas-solid separation system is represented by a cyclone separator (22〇), but any other gas-solid separation system may be used, for example, a separation device at the upper end of the standpipe (210) may be designed, such as three Pass through the tube and it is within the scope of the reaction zone of the invention. The separator (220) can generally cover at least 70% of the solid particles, which can be reintroduced into the main reactor via the outlet (222) of the separator, the outlet of which is close to the main reactor (100) The fluidized bed level of the stripping zone (121). 131895.doc -22- 200911975 The term "proximity" means that the stripping zone (121) of the primary reactor (100) has a distance of about 5 meters above or below the level of the dense bed, preferably about 3 meters. The cleaned effluent (221) is reintroduced into the dilute phase (11 〇) of the main reactor (100) at any level of the dilute phase (110), but is preferably introduced into the upper portion of the zone. Since the temperature of the additional riser (210) is generally substantially higher than the temperature of the main riser (1〇), the injection quench fluid (230) can limit the temperature of the effluent (221) f

度。一般將此驟冷流體引入分離裝置（220)之出口管線中。因此，可能使排出物（221)足夠冷卻以防止其於額外豎官（21 0)之下游熱降解。源自額外豎管（21〇)之經冷卻排出物冲洗主要反應器（1〇〇)之稀釋區（丨1〇)且穿過汽提腔室（3〇) 之開口 (26)，於開口處其與源自主要反應器(1〇〇)之氣態排出物聯合。注射驟冷流體（23〇)不出物的溫度，且亦可將來自主要豐管（1〇)之排出物的溫度降低至令人滿意之水平，其可降低待注射至主要反應器 (⑽)的稀釋區（11G)中之驟冷流體⑽）的量。在—些情況下，視情況可省卻驟冷流體（105)。 (二有來自額外登管(21°)之排出物之驟冷流體、^而/要s f中之排出物溫度降低至汽提腔室⑽之之情況亦如此。此Μ Ή的·度’使用流體（H)5) J戈此此增加兩種氣態排出物（―種A6 + 登管之"熱”排出物，且另一種為自額㈣=來自主要卻排出物）之間p a * 貞夕卜w到達之已經冷吧合效率。此優勢極重要，因為因而有 131895.doc •23- 200911975 可月b比先月才支術更有效地（亦即在無需汽化驟冷液體（1 〇5) 下）降低/*L提腔至（3〇)上游的反應排出物之溫度，因為已經 Ό之來自額外g官之排出物（亦即以驟冷流⑺…補充之流（22 1))均為蒸氣狀態。 ' 本^月之另一優勢為憑藉此裝置，適當地沖洗主要反庫、degree. This quench fluid is typically introduced into the outlet line of the separation unit (220). Therefore, it is possible to cool the effluent (221) sufficiently to prevent thermal degradation downstream of the additional erection (21 0). The cooled effluent from the additional standpipe (21〇) rinses the dilution zone (丨1〇) of the main reactor (1〇〇) and passes through the opening (26) of the stripping chamber (3〇) at the opening It is combined with a gaseous effluent from the main reactor (1〇〇). The quenching fluid (23 〇) is injected without the temperature of the material, and the temperature of the effluent from the main tube (1 〇) can also be lowered to a satisfactory level, which can reduce the injection to be injected into the main reactor ((10) The amount of quenching fluid (10) in the dilution zone (11G). In some cases, the quench fluid (105) may be omitted as appropriate. (2) The quenching fluid from the effluent from the additional pipe (21°), or the temperature of the effluent in the sf is reduced to the stripping chamber (10). This Μ Fluid (H) 5) J Ge adds two gaseous effluents ("A6 + enthalpy" "heat" effluent, and the other is self-valued (four) = from the main effluent) between pa * 贞夕卜w has reached the cold and the efficiency. This advantage is extremely important, because there is 131895.doc •23- 200911975 can be more effective than the first month of the branch (that is, without the need to vaporize the quench liquid (1 〇 5 Lower) lowers the temperature of the reaction effluent upstream of the (*3) chamber to (3〇) because the effluent from the additional g official (ie, the stream replenished by the quenching stream (7)... (22 1)) All are in a vapor state. 'Another advantage of this ^ month is that with this device, the main anti-reservoir is properly flushed,

. 印叫之稀釋區⑽），且藉由注射驟冷流體（230)將其I 度保持在控制下。實際上’主要反應器之稀釋區（110)之溫纟低於40(rc為不合理的’因為在此溫度下大幅增加烴氣態排出物漠縮之危險。使用來自額外-或多個g管（210)之排出物/中洗主要反應器之稀釋相⑴的優勢為由於注射來自額外-或多個g管之出口的驟冷流體（23〇)，此排出物之 μ度足夠低至限制熱降解’且此溫度亦足夠高至限制烴濃縮之危險。在實踐中，在注射驟冷流體（230)之後，來自額外一或多個豎管之排出物溫度在5〇〇ti55(rc之範圍内。本發明之反應區與先前技術相比經改良，因為在先前技 y 術跟心中必而主射沖洗流體（諸如蒸汽（104))來沖洗稀釋區（11 〇)'而，低冲洗蒸汽（104)流動速率一般導致不良沖洗反應器（100)之稀釋區（11〇)且高流動速率之蒸汽導致優良沖洗’但具有使稀釋區（11〇)過分冷卻之危險。因 ' 此，在先前技術中難以調節沖洗（104)流動速率。本电明裝置可克服此缺陷，因為來自額外豎管（2 1 〇)之反應排出物（221)可替換大部分（亦即至少7〇%，且較佳地至少80/。）之沖洗流體（1〇4)。在一些情況下，沖洗流體 (104)甚至可全部經替換。 131895.doc -24- 200911975 此外，藉由驟冷流體（230)之量來調節沖洗氣體之溫度。首先，本發明裝置可使確保充分沖洗主要反應器（1 〇〇) 之稀釋區（110)所需之量之沖洗流體去耗合。其次，於稀釋區（110)中循環之排出物溫度基本上由驟冷流體（230)所控制。此景〉響之一般結果為大部分（亦即超過7〇%且較佳地超過 80%之程度）可經與來自額外一或多個豎管之排出物（221) 一起注射之驟冷流體（230)替換的主要反應器（1〇〇)中之驟冷流體（1 0 5 )之流動速率降低。在圖2中，吾人展示本發明之另一實施例，其與描述於圖1中之實施例之間的差異為來自額外豎管（210)之反應排出物（250)不經受初始分離且係直接傳送至主要反應器 (100)之稀釋區（110)中。現在額外豎管（21 0)之出口處，對來自額外豎管（2 1 〇)之全部排出物（250)進行驟冷（230)。接著，藉由於主要反應器（100)之稀釋區（11〇)中進行沈澱而天然地進行氣-固分離。因此，有必要注射較大量之驟冷流體（230)以於稀釋區（11〇)中達到相同溫度，接著冷卻不僅涉及蒸氣，且亦涉及於額外反應器（21〇)之反應區中循環之全部催化劑。本發明之實例為說明實施本發明之優點，使用自預備單元實驗按比例增加之方法模型，吾人模擬藉由進行特徵描述於表1中之 131895.doc -25- 200911975 重餾分的催化裂化而獲得之效能。饋料為至少9〇%在36〇。(：以上經蒸館之未經氫處理之常廢殘餘物。殘餘物之密度為935 kg/m3，且氫含量為121重量％。重饋料之康拉特遜碳為5,7重量％。需要再生區中之熱交換器（催化冷卻器）來形成單元之熱平衡。 … 15C下之密度 935 kg/mJ 晒---—- 平均沸點 503。。氫含量 ^2.1重量％硫含量 Τό7 重量％ ~~~ 氮含量 0.15重量％一康拉特遜碳 - 5.7重量％表1 :餚料特徵The dilution zone (10) is printed and the I degree is maintained under control by injection of quench fluid (230). In fact, the temperature of the dilution zone (110) of the main reactor is below 40 (rc is unreasonable 'because the danger of hydrocarbon gas venting is greatly increased at this temperature. Use from extra- or multiple g-tubes The advantage of the dilute phase (1) of the effluent/intermediate main reactor of (210) is that the effluent μ is sufficiently low to limit the injection due to the quenching fluid (23 〇) from the outlet of the extra- or multiple g-tubes. Thermal degradation 'and this temperature is also high enough to limit the risk of hydrocarbon concentration. In practice, after injection of the quench fluid (230), the temperature of the effluent from the additional one or more standpipes is 5 〇〇 ti55 (rc The reaction zone of the present invention is improved over the prior art because in the prior art, the flushing fluid (such as steam (104)) is required to flush the dilution zone (11 〇), while the low flushing The steam (104) flow rate generally results in a poor dilution zone (11〇) of the flushing reactor (100) and a high flow rate of steam results in an excellent flushing' but with the risk of excessively cooling the dilution zone (11〇). It is difficult to adjust the rinsing (104) flow in the prior art The present device overcomes this drawback because the reaction effluent (221) from the additional standpipe (2 1 〇) can replace most (i.e., at least 7%, and preferably at least 80%). Flushing fluid (1〇4). In some cases, the flushing fluid (104) may even be replaced. 131895.doc -24- 200911975 In addition, the temperature of the flushing gas is adjusted by the amount of quenching fluid (230). First, the apparatus of the present invention can be used to ensure that the flushing fluid required to adequately flush the dilution zone (110) of the primary reactor (110) is depleted. Second, the temperature of the effluent circulated in the dilution zone (110) is substantially Controlled by the quenching fluid (230). The general result of this sounding is that most (i.e., more than 7% and preferably more than 80%) may be passed from the other one or more risers. The flow rate of the quenching fluid (105) in the main reactor (1) in which the effluent (221) is injected together with the quenching fluid (230) is reduced. In Figure 2, we show another An embodiment, the difference from the embodiment described in Figure 1 is from The reaction effluent (250) of the standpipe (210) is not subjected to the initial separation and is transferred directly to the dilution zone (110) of the main reactor (100). Now the outlet of the additional standpipe (21 0) is from the extra The entire effluent (250) of the standpipe (2 1 〇) is quenched (230). Next, the gas-solid separation is naturally carried out by precipitation in the dilution zone (11 Torr) of the main reactor (100). Therefore, it is necessary to inject a larger amount of quenching fluid (230) to reach the same temperature in the dilution zone (11 Torr), followed by cooling involving not only steam but also in the reaction zone of the additional reactor (21 Torr). All catalysts. An example of the invention is illustrative of the advantages of practicing the invention, using a method of scaled up from a preliminary unit experiment, which was simulated by catalytic cracking of the heavy fractions of 131895.doc-25-200911975 characterized in Table 1. Performance. The feed is at least 9〇% at 36〇. (: The above-mentioned waste residue of the steaming plant without hydrogen treatment. The density of the residue is 935 kg/m3, and the hydrogen content is 121% by weight. The Conradson carbon of the heavy feed is 5,7 wt% The heat exchanger (catalytic cooler) in the regeneration zone is required to form the heat balance of the unit. ... The density at 15C is 935 kg/mJ. The average boiling point is 503. Hydrogen content ^ 2.1% by weight Sulfur content Τό 7 Weight % ~~~ Nitrogen content 0.15 wt% One Conradson carbon - 5.7 wt% Table 1: Characteristics of the food

U 用於所有實例中之催化劑為以150 m2/g活性表面積（其中 75%在沸石+且25%在基f中）為特徵之含有超穩定麟沸石之平衡催化劑。平衡催化劑中之重金屬含量為4〇〇〇 ppm V及 2000 ppm Ni。模擬多種組態以最佳說明本申請案中所述之本發明優勢0 實例1B係根據先前技術’因為其僅包括一個加工表1之重饋料之主要豎管。實例2B、3B及4B亦係根據先前技術，因為其對應於在不與主要豎官耦合之額外豎管中加工來自主要豎管之再循環餾分。 131895.doc -26 · 200911975 實me、3C及4C係根據本發明，因為其對應於在額外賢管中加1源…豎管之再循環衫，該額外登管此時與根據本發明之主要豎管耦合。 τ 實例1Β(先前技術）在實例财’吾人使用單一反應器(在其上端具備快速分離系統，諸如參考圖丨所描述者）模擬描述於表1中之重饋料之催化裂化。U The catalyst used in all the examples was an equilibrium catalyst containing ultrastable shale as characterized by an active surface area of 150 m2/g (75% in zeolite + and 25% in base f). The heavy metal content of the equilibrium catalyst is 4 〇〇〇 ppm V and 2000 ppm Ni. A variety of configurations are simulated to best illustrate the advantages of the present invention described in this application. Example 1B is based on the prior art 'because it includes only one primary riser that processes the heavy feed of Table 1. Examples 2B, 3B, and 4B are also according to the prior art because they correspond to processing a recirculating fraction from the main standpipe in an additional standpipe that is not coupled to the main stand. 131895.doc -26 · 200911975 实me, 3C and 4C are according to the invention, since it corresponds to a recirculating shirt with 1 source...standpipe added to the extra sage, this additional tube is now at the same time according to the invention The standpipe is coupled. τ Example 1 (Prior Art) In the example, a single reactor (having a fast separation system at its upper end, such as described with reference to Figure 模拟) simulates the catalytic cracking of the heavy feed described in Table 1.

將此實例之值用作確定本發明效應之參照： 294 t/h 545〇C 525〇C 485〇C 5.0 43.9重量％ 8.6重量％ 4.3重量％ 70,4重量％ 16.4 t/h 主要豎管饋料流動速率主要豎管出口處之溫度驟冷後主要豎管出口處之溫度稀釋相之平均溫度 e/ο比率汽油產生（C5-220°C ) 焦炭產生丙婦產生總轉化率驟冷流體流動速率，L c 〇 (1 〇 5) 沖洗流體、蒸汽流動速率（104) 2.5 t/h 自再生器提取之熱量（催化冷卻器）4250〇xl〇0eal/h 實例2(比較）在實例2中’吾人模擬主要豎管中重饋料之催化裂化及 131895.doc • 27- 200911975 額外豎管中輕餾分之催化裂化，該額外豎管獨立於主要豎管（先前技術情況2B)或如本發明中耦合至主要豎管（情況 2C，根據本發明）。再循環至額外豎管中之餾分係由以下排出物構成： •源自主要重饋料轉化豎管之C6 + 220°C汽油餾分，於該複合設備中產生之50%汽油係由經再循環之兩個反應器構成； •主要由含有至少8個碳原子之長鏈烯烴構成之寡聚汽油餾分，其係由於使主要重饋料轉化反應器中產生之所有C4及C5餾分寡聚而產生。 2B (先前技術） 2C (inv) 主要豎管新鮮饋料流動速率 294 t/h 294 t/h 再循環至第二豎管中之輕饋料流動速率 135 t/h 135 t/h 主要豎管出口處之溫度(T1) 545 °C 545 V 額外豎管出口溫度(T2) 590〇C 590°C 驟冷後之主要豎管溫度(T3) 525。。 525 r 驟冷後之額外豎管溫度(T4) 525〇C 510°C 來自主要反應器之稀釋相之平均溫度(T5) 485〇C 510 V 額外反應器之稀釋相之平均溫度 520〇C 無關 C/0比率，主要豎管 5.1 5.2 C/0比率，第二豎管 7.5 8.0 汽油產生(C5-220°C) 40.1% 40.3% 焦炭產生 9.6% 9.5% 丙烯產生 7.4% 7.9% 總轉化率 69.4% 70.2% 主要反應器中驟冷流體(105)之流動速率 16.5 T/h 8.0 T/h 額外豎管中驟冷流體之流動速率 27.4 T/h 36.9 T/h 主要豎管周圍之稀釋相中沖洗流體(104)流動速率 2.5 T/h OT/h 額外豎管周圍之稀釋相中沖洗流體(104)之流動速率 2.0 T/h (〇)無關再生器處提取之熱量(催化冷卻器） 0 Mcal/h 0 Mcal/h 在實例2中，吾人發現辆合兩個豎管使汽油產生及丙稀產生皆增加。由於涉及B頓位，故0.5點丙烯增加極其顯著。 131895.doc •28- 200911975 _亦可見驟冷流體於主要暨管與額外豐管之間之流動分配 2改變’ 82%之驟冷流體係注射至額外豎管中，其意謂在 h况2C中可省部沖洗流體’且可更有效地控制額外登管出口處之反應終止。 - 驟冷後之溫度㈣為5阶而非5饥，而一般出口溫度 (T3)保持 525°C。主要反應器之稀釋相之溫度（T5)現為5i〇r而非48yc， (〃 Ή可於稀釋相中維持合理溫度，同時保持比情況28中冑得多的沖洗流動速率，在情㈣中僅以25t/h蒸氣沖洗稀釋相。々沖洗流動速率對應於第二豎管之饋料流動速率及額外賢管之驟冷流動速率，亦即約丨8〇 t/h。不再有必要沖洗額外豎管周圍之稀釋相。比較情況2B與2C亦展示整合本發明之快速分離及驟冷系統可增加催化劑循環（㈣，其在主要賢管中自51變化〇至5·2 ’且在第二豎管中自7.5變化至8.〇。亦可見不再有必要如1B之情況巾❹催化冷卻器自再生 ϋ提取熱量，裂化第二置f中之輕饋料使得自總反應區提取足夠熱量。實例3(比較）在實例3中，吾人模擬主要暨管中重饋料之催化裂化，及額外豐管中若干輕館分之催化裂化，該額外賢管獨立於主要登管(先前技術情況3B)或與主要登管耗合(情況I 根據本發明）。 131895.doc -29- 200911975 再循環至額外豎管之顧分係由下列排出物構成： • a)源自主要重饋料轉化豎管之C6 + -220汽油餾分，由兩個豎管構成之複合設備中所產生之75%汽油經再循環； • b)主要由含有至少8個碳原子之長鏈烯烴構成之寡聚汽油餾分，其係由於使主要重饋料轉化反應器中產生之所有C4及C5餾分寡聚而產生； • c)由兩個豎管構成之反應器產生之50% LCO餾分，其蒸餾範圍為220°C至36CTC。 3B (先前技術） 3C (inv) 主要豎管新鮮饋料流動速率 294 t/h 294 t/h 再循環至第二豎管之輕饋料流動速率 230 t/h 230 t/h 主要豎管出口溫度(T1) 545〇C 545〇C 額外豎管出口溫度(T2) 590〇C 590〇C 驟冷後之主要豎管溫度(T3) 525〇C 525。。驟冷後之額外豎管温度(T4) 525〇C 510°C 來自主要反應器之稀釋相之平均溫度(T5) 485。。 510°C 額外反應器之稀釋相之平均溫度 520〇C 無關 C/Ο比率，主要豎管 8.8 9.3 C/Ο比率，第二豎管 13.7 14.6 汽油產生(C5-22(TC) 31% 30.9% 焦炭產生 12.4% 12.1% 丙烤產生 16.1% 17.2% 總轉化率 82.6% 82.8% 主要反應器中驟冷流體(105)之流動速率 18.6 T/h 3.6 T/h 額外豎管中驟冷流體(230)之流動速率 50.4 T/h 64.2 T/h 主要豎管周圍之稀釋相中沖洗流體(104)之流動速率 2.5 T/h OT/h 額外豎管周圍之稀釋相中沖洗流體(104)之流動速率 2.0 T/h (〇)無關在實例3中，吾人發現耦合兩個豎管使汽油產生及丙烯產生皆增加。由於涉及噸位，故1.1點丙烯增加極其顯著。亦可見驟冷流體於主要豎管與額外豎管之間之流動分配 131895.doc -30- 200911975 經改變。 =反應器之稀釋相之溫度⑽現為51代而非4src， …“可於稀釋相中使溫度保持合理水平，同時具有比情況3B中高得多的沖率，在情況腳僅以2.5 t/h蒸氣沖洗稀釋相。 —中U速率對應於第二豐管之饋料流動速率及額外登管之驟冷流動速率，亦即約295 t/h。不再有必要沖洗額外登管周圍之稀釋相。比較情況3 B與3 C展千敕人a L展不整合本發明之快速分離及驟冷系統可由於咖制環Μ加MS管巾之催化劑循環（c/0 自8.8變化至9.3)，日丄i 了 s加主要豎管中及第二豎管中之催化裂化量（(：/〇自13.7變化至14 6)。二亦發現不再有必要如1B之情況中使用催化冷卻器自再生 -提取’’、、s g為裂化第二豎管中之輕饋料使得自總反應區提取足夠熱量。實例4(比較）在實例4中吾人核擬主要賢管中重饋料之摧化裂化，及額外豎管中料輕饋料之催化裂化，該額外S管獨立於主要豎官（先前技術情況4B)或如本發明與主要g管輕合⑽ 況4C’根據本發明）。再循環至額外t管之❹係由下列排出物構成： •源自主要重饋料轉化豎管之C6+22(rc汽油館分，由兩個反應器構成之複合設備中所產生之25%汽油經再循環（與實例2中之5〇%相對）； 13I895.doc 200911975 •主要由含有至少8個碳原子之長鏈烯烴構成之寡聚汽油餾分，其係由於使主要重饋料轉化反應器中產生之所有C4及C5餾分寡聚而產生； •由以62 t/h之流動速率供應至第二豎管且具有53%含烯度之鏈之C1 8甘油三醋結構的豆油構成之烴德分。在此等條件下，第二豎管中之輕烴流動速率為恆定的且係由73 t/h之來自FCC及將C4-C5烯烴與聚石油腦寡聚之汽油及62 t/h之豆油構成。 4B (先前技術）4C (inv) 主要豎管新鮮饋料流動速率 294 t/h 294 t/h 再循環至第二豎管之輕饋料流動速率 73 t/h 73 t/h 至第二豎管之新鮮饋料流動速率 62 t/h 62 t/h 主要豎管出口之溫度(T1) 545〇C 545 °C 額外豎管出口溫度(T2) 590〇C 590〇C 驟冷後之主要豎管溫度(T3) 525°C 525。。驟冷後之額外豎管溫度(T4) 525 °C 51(TC 來自主要反應器之稀釋相之平均溫度(T5) 485〇C 510°C 額外反應器之稀釋相之平均溫度 520〇C 無關 C/0比率，主要豎管 4.9 5.1 C/0比率，第二豎管 7.2 7.7 汽油產生(C5-220°C) 42.1% 42.4% 焦炭產生 9.7% 9.6% 丙稀產生 6.9% 7.4% 主要反應器中驟冷流體(105)之流動速率 16.3 T/h 7.8 T/h 額外豎管中驟冷流體之流動速率 27.1 T/h 36.6 T/h 主要豎管周圍之稀釋相中沖洗流體(104)之流動速率 2.5 T/h OT/h 額外豎管周圍之稀釋相中沖洗流體(104)之流動速率 2.0 T/h (〇)無關在再生器處提取之熱量(催化冷卻器） 0 Mcal/h 0 Mcal/h 在實例4中，吾人發現耦合兩個豎管亦使汽油產生及丙烯產生皆增加。由於涉及噸位，故0.5點丙烯增加極其顯著。亦可見驟冷流體於主要豎管與額外豎管之間之流動分配經改變，82%之驟冷流體係注射至額外豎管中，其意謂在 131895.doc -32- 200911975The value of this example was used as a reference for determining the effect of the invention: 294 t/h 545 〇C 525 〇C 485 〇C 5.0 43.9 wt% 8.6 wt% 4.3 wt% 70,4 wt% 16.4 t/h main standpipe feed Feed flow rate The temperature at the outlet of the main standpipe is quenched. The average temperature of the temperature dilute phase at the outlet of the main standpipe is e/ο ratio of gasoline produced (C5-220 ° C). The total conversion rate of coke produced by coke is quench fluid. Flow rate, L c 〇(1 〇5) Flushing fluid, steam flow rate (104) 2.5 t/h Heat extracted from the regenerator (catalytic cooler) 4250〇xl〇0eal/h Example 2 (comparative) In Example 2 In the 'Human simulation of catalytic cracking of heavy feeds in the main standpipe and 131895.doc • 27- 200911975 Catalytic cracking of light ends in additional standpipes, independent of the main standpipe (previous technical case 2B) or as In the invention, it is coupled to the main standpipe (case 2C, in accordance with the invention). The fraction recycled to the additional standpipe consists of the following effluents: • C6 + 220 °C gasoline fraction from the main heavy feed conversion standpipe, 50% of the gasoline produced in the composite plant is recycled The two reactors are constructed; • an oligomeric gasoline fraction consisting mainly of long chain olefins having at least 8 carbon atoms, which is produced by oligomerizing all of the C4 and C5 fractions produced in the main feedstock conversion reactor. . 2B (prior art) 2C (inv) main standpipe fresh feed flow rate 294 t/h 294 t/h light feed flow rate recirculated to the second standpipe 135 t/h 135 t/h main standpipe Temperature at the exit (T1) 545 °C 545 V Extra standpipe outlet temperature (T2) 590〇C 590°C Main standpipe temperature (T3) 525 after quenching. . 525 r Additional standpipe temperature after quenching (T4) 525〇C 510°C Average temperature of the diluted phase from the main reactor (T5) 485〇C 510 V The average temperature of the diluted phase of the additional reactor is 520〇C C/0 ratio, main standpipe 5.1 5.2 C/0 ratio, second standpipe 7.5 8.0 gasoline production (C5-220°C) 40.1% 40.3% coke yield 9.6% 9.5% propylene yield 7.4% 7.9% total conversion rate 69.4 % 70.2% Flow rate of quench fluid (105) in the main reactor 16.5 T/h 8.0 T/h Flow rate of quench fluid in additional standpipe 27.4 T/h 36.9 T/h Dilution phase around main standpipe Flushing fluid (104) flow rate 2.5 T / h OT / h The flow rate of the flushing fluid (104) in the dilute phase around the additional standpipe 2.0 T / h (〇) irrelevant heat extracted at the regenerator (catalytic cooler) 0 Mcal/h 0 Mcal/h In Example 2, we found that the combination of two standpipes increased both gasoline production and propylene production. Since the B-position is involved, the increase in propylene at 0.5 point is extremely significant. 131895.doc •28- 200911975 _Also see the flow distribution of quench fluid between the main cum tube and the extra plumbing 2 change '82% of the quenching system injection into the additional standpipe, which means 2C in h The province can flush the fluid' and can more effectively control the termination of the reaction at the exit of the additional tube. - The temperature after quenching (4) is 5th order instead of 5 hunger, while the general outlet temperature (T3) is 525 °C. The temperature of the dilute phase of the main reactor (T5) is now 5i〇r instead of 48yc, (〃 Ή can maintain a reasonable temperature in the diluted phase while maintaining a much higher flush flow rate than in case 28, in case (4) The dilution phase is only flushed with 25 t/h of steam. The rinsing flow rate corresponds to the feed flow rate of the second standpipe and the quench flow rate of the additional squid, ie about 8 〇t/h. Dilution phase around the additional standpipe. Comparisons 2B and 2C also show that the rapid separation and quenching system of the present invention can increase the catalyst cycle ((iv), which varies from 51 to 5·2 in the main sage and is in In the second standpipe, the change from 7.5 to 8. 〇. It can be seen that it is no longer necessary to extract heat from the regeneration enthalpy as in the case of 1B, and crack the light feed in the second set f to make enough extraction from the total reaction zone. Heat. Example 3 (Comparative) In Example 3, we simulated the catalytic cracking of the heavy feed in the main cum tube, and the catalytic cracking of several light parts in the extra tube, which is independent of the main tube (previous technique) Case 3B) or with major boarding (case I) According to the invention) 131895.doc -29- 200911975 The recycling of the additional standpipe consists of the following effluents: • a) C6 + -220 gasoline fraction derived from the main heavy feed conversion standpipe, consisting of two 75% of the gasoline produced in the composite equipment consisting of a riser is recycled; • b) an oligomeric gasoline fraction consisting mainly of long-chain olefins containing at least 8 carbon atoms due to the conversion of the main heavy feed All C4 and C5 fractions produced in the reactor are oligomerized to produce; • c) 50% LCO fraction produced by a reactor consisting of two standpipes with a distillation range of 220 °C to 36 CTC. 3B (prior art) 3C (inv) main standpipe fresh feed flow rate 294 t/h 294 t/h light feed flow rate recirculated to the second standpipe 230 t/h 230 t/h main riser outlet Temperature (T1) 545〇C 545〇C Extra standpipe outlet temperature (T2) 590〇C 590〇C Main standpipe temperature after quenching (T3) 525〇C 525. . Additional standpipe temperature after quenching (T4) 525 〇C 510 °C Average temperature (T5) 485 from the dilute phase of the main reactor. . 510 ° C The average temperature of the diluted phase of the additional reactor is 520 〇 C. The C/Ο ratio is not related, the main standpipe is 8.8 9.3 C/Ο ratio, the second standpipe is 13.7 14.6 Gasoline is produced (C5-22(TC) 31% 30.9% Coke production 12.4% 12.1% Propylene roasting 16.1% 17.2% Total conversion 82.6% 82.8% Flow rate of quenching fluid (105) in the main reactor 18.6 T/h 3.6 T/h Additional quenching fluid in the standpipe (230 Flow rate 50.4 T/h 64.2 T/h Flow rate of flushing fluid (104) in the dilute phase around the main standpipe 2.5 T/h OT/h Flow of flushing fluid (104) in the dilute phase around the additional standpipe Rate 2.0 T/h (〇) Irrelevant In Example 3, we found that coupling two risers increased both gasoline production and propylene production. Due to the tonnage involved, the 1.1 point propylene increase was extremely significant. It can also be seen that the quench fluid is mainly vertical. The flow distribution between the tube and the additional standpipe 131895.doc -30- 200911975 is changed. = The temperature of the diluted phase of the reactor (10) is now 51 generations instead of 4src, ... "the temperature can be kept at a reasonable level in the diluted phase, At the same time, it has a much higher impulse rate than in case 3B. In the case, the foot is only 2.5 t/h. The vapor flushes the diluted phase. - The medium U rate corresponds to the feed flow rate of the second tube and the quenching flow rate of the additional tube, ie about 295 t/h. It is no longer necessary to rinse the diluted phase around the additional tube. Comparative situation 3 B and 3 C exhibition Millennium A L exhibition unconformity The rapid separation and quenching system of the present invention can be cycled by the catalyst loop of the coffee ring and the MS tube (c/0 changed from 8.8 to 9.3). The amount of catalytic cracking in the main riser and the second riser ((:/〇 varies from 13.7 to 14 6) is also found. It is also found that it is no longer necessary to use a catalytic cooler since the case of 1B. Regeneration-extraction '', sg is the light feed in the cracked second standpipe to extract enough heat from the total reaction zone. Example 4 (Comparative) In Example 4, we verified the destruction of heavy feedstock in the main sage Cracking, and catalytic cracking of the light feed of the additional riser, which is independent of the main vertical (previous technical case 4B) or as the present invention is lightly combined with the primary g (10) 4C' according to the invention). The enthalpy that circulates to the extra t-tube consists of the following effluents: • From the main heavy feed conversion riser C6+22 (rc gasoline hall, 25% of the gasoline produced in the composite equipment consisting of two reactors is recycled (as opposed to 5〇% in Example 2); 13I895.doc 200911975 • mainly consists of at least 8 An oligomeric gasoline fraction composed of long chain olefins of one carbon atom, which is produced by oligomerizing all of the C4 and C5 fractions produced in the main heavy feed conversion reactor; • supplied to the flow rate of 62 t/h The second standpipe and the hydrocarbon residue of the C1 8 glycerol triacetate structure of the 53% olefinic chain. Under these conditions, the light hydrocarbon flow rate in the second standpipe is constant and is from 73 t/h of FCC from the FCC and the C4-C5 olefin to the polyoleocephalon and 62 t/h of soybean oil. Composition. 4B (prior art) 4C (inv) main standpipe fresh feed flow rate 294 t/h 294 t/h recirculating to the second standpipe light feed flow rate 73 t/h 73 t/h to second vertical Fresh feed flow rate of tube 62 t/h 62 t/h Temperature of main standpipe outlet (T1) 545〇C 545 °C Extra standpipe outlet temperature (T2) 590〇C 590〇C Main vertical after quenching Tube temperature (T3) 525 °C 525. . Additional standpipe temperature after quenching (T4) 525 °C 51 (TC average temperature from the dilute phase of the main reactor (T5) 485 〇C 510 °C Average temperature of the diluted phase of the additional reactor 520 〇C Irrelevant C /0 ratio, main standpipe 4.9 5.1 C/0 ratio, second standpipe 7.2 7.7 gasoline production (C5-220 °C) 42.1% 42.4% coke yield 9.7% 9.6% propylene production 6.9% 7.4% Main reactor Flow rate of quench fluid (105) 16.3 T/h 7.8 T/h Flow rate of quench fluid in additional standpipe 27.1 T/h 36.6 T/h Flow of flushing fluid (104) in the dilute phase around the main standpipe Rate 2.5 T/h OT/h Flow rate of the flushing fluid (104) in the dilute phase around the additional standpipe 2.0 T/h (〇) Irrelevant heat extracted at the regenerator (catalytic cooler) 0 Mcal/h 0 Mcal /h In Example 4, we found that coupling two risers also increased both gasoline production and propylene production. Due to the tonnage involved, the increase in propylene at 0.5 point is extremely significant. It can also be seen that the quench fluid is in the main riser and the additional riser. The flow distribution between the two was changed, and 82% of the quenching system was injected into the additional standpipe, which means at 131895 .doc -32- 200911975

It况4C中可省部沖洗流體，且可更有效地控制額外豎管出口處之反應結束。驟冷後之溫度（T4)為510°C而非525t，而一般出口溫度 (T3)保持 525°C。主要反應器之稀釋相之溫度（T5)現為51代而非485忙，其意謂可於稀釋相中維持合理溫度，㈣保持比情況化中高得多的沖洗流動速率，在情㈣中僅以25麟氣沖洗稀釋相。时沖洗流動速率對應於第二賢管之饋料流動速率及額外賢官之驟冷流動速率，亦即約丨8〇 t/h。不再有必要沖洗額外豎管周圍之稀釋相。較It况4B與4C進一步展示整合本發明之快速分離及驟冷糸統可增加催化劍維· jss n lr\ 4- 惟亿削循％，（:/〇在主要豎管中自4.9變化至5.1，且在第二豎管令自72變化至77。亦可見不再有必要如1B之情況中使用催化冷卻器自再生績取熱量’因為裂化第二置管中之輕饋料使得自總反應區提取足夠熱量。【圖式簡單說明】 …圖1根據本發明描述包含兩個豎管之反應區，該兩個登 2用於裂化重餾分之主要賢管及用於裂化輕館分之額外 :使來自額外t f之氣_固排出物以兩部分排至主要，'器中’其中-部分基本上為氣態，其排至該主要反應 :之卿相中’其中其與來自主要登管之排出物混合，而 …基本上為固態的’其排至主要反應器之敏密相 131895.doc •33· 200911975 中。々圖2根據本發明描述包含兩個賢管之反應區；該兩個权 ::用於裂化重餾分之主要賢管及用於裂化輕餾分之額：丑吕來自額外置官之氣態及固態排出物在未分離下— 排出至主要反應器之稀釋相中。【主要元件符號說明】 1 來自再生區之再生催化劑In the case of 4C, the province can flush the fluid and control the end of the reaction at the outlet of the additional standpipe more effectively. The temperature after quenching (T4) is 510 ° C instead of 525 t, while the general outlet temperature (T3) is maintained at 525 ° C. The temperature of the dilute phase of the main reactor (T5) is now 51 generations rather than 485 busy, which means that a reasonable temperature can be maintained in the diluted phase, and (iv) maintain a much higher flushing flow rate than in the case, in case (4) only Rinse the diluted phase with 25 lin. The flushing flow rate corresponds to the feed flow rate of the second sump and the additional quenching flow rate of the sage, i.e., about 8 〇 t/h. It is no longer necessary to rinse the dilute phase around the additional standpipe. It is further demonstrated that the rapid separation and quenching system of the present invention can increase the catalysis of the Jianwei·jss n lr\ 4- 削削 , , , , , , , , , , , , , , , , , , , , , , , , , , , 4- 4- 4- 4- 4- 4- 4- 4- 4- 5.1, and in the second standpipe change from 72 to 77. It can also be seen that it is no longer necessary to use the catalytic cooler to take heat from the regeneration as in the case of 1B' because the light feed in the second pipe is cracked. The reaction zone extracts enough heat. [Simplified illustration of the drawing] Fig. 1 depicts a reaction zone comprising two risers for the cracking of the main sump of the heavy fraction and for the cracking of the lighthouse according to the present invention. Extra: the gas-solid effluent from the extra tf is discharged in two parts to the main, where the - part is essentially gaseous, which is discharged into the main reaction: the phase of the 'in which it is associated with the main The effluent is mixed, and ... is substantially solid - it is discharged into the dense phase of the main reactor 131895.doc • 33· 200911975. Figure 2 depicts a reaction zone comprising two sage tubes according to the present invention; Ownership:: Mainly used for cracking heavy fractions and used for cracking light distillation Amount of: Lu ugly and solid effluent gas from the additional set of at unseparated officer - discharged to the primary reactor dilute phase main element of [1] Symbol Description regenerated catalyst from the regeneration zone.

10 主要豎管 /主射基本上軋態之流體（蒸汽，輕分 12 可使液態之該饋料霧化成精細液滴之構件/重饋料 13 14 20 21 22 23 25 26 29 30 40 女置於重饋料（12)之注射點下游（反應流體的流動方向）之構件/液體女置於重饋料（12)之注射點下游（反應流體的流動方向）之構件/液體分離腔室分離腔室（20)之入口部分分離腔室（20)之出口部分偏導器與相鄰汽提腔室（30)連通之開口位於汽提腔室（30)下部之開口位於汽提腔室（30)上部之共同開口汽提腔室垂直管線 131895.doc -34· 機械構件垂直管線漩渦分離器/第二分離系統管線水平管線/高速率流動區管線進行重饋料之催化裂化之主要反應器一般置放於反應器（100)頂部之管線汽提蒸氣用以接合再生區之管線蒸汽/沖洗流體主要反應器（100)中之驟冷流體主要反應器（100)之稀釋區汽提蒸氣主要反應器（100)之緻密相區引入蒸汽之水平内部裝填元件催化劑流額外豎管基本上氣態之流體輕饋料/待裂化之輕餾分初始氣-固分離器額外豎管（2 10)之反應排出物裂化催化劑 -35- 200911975 230 與來自額外一或多個豎管之排出物（221)—起注射之驟冷流體 250 來自額外豎管（2 10)之反應排出物 131895.doc -36-10 Main standpipe/main shots are basically rolled fluids (steam, light fraction 12 can be used to atomize the liquid feed into fine droplets / heavy feed 13 14 20 21 22 23 25 26 29 30 40 The member/liquid separation chamber downstream of the injection point of the heavy feed (12) (the flow direction of the reaction fluid) is separated from the component/liquid female downstream of the injection point of the heavy feed (12) (flow direction of the reaction fluid) The outlet portion of the chamber (20) is separated from the outlet portion of the chamber (20). The opening of the deflector is connected to the adjacent stripping chamber (30). The opening at the lower portion of the stripping chamber (30) is located in the stripping chamber ( 30) Upper common open stripping chamber vertical line 131895.doc -34 · Mechanical component vertical line vortex separator / second separation system line horizontal line / high rate flow area line Main reactor for catalytic cracking of heavy feed The line stripping steam generally placed at the top of the reactor (100) is used to join the regeneration zone. The steam/flushing fluid in the main reactor (100) is quenched in the main reactor (100). Reactor (100) The dense phase zone introduces the level of steam. Internal loading element Catalyst flow Additional standpipes Substantially gaseous fluid Light feedstock / Light fraction to be cracked Initial gas-solids separator Additional riser (2 10) Reaction effluent Cracking catalyst -35 - 200911975 230 The quench fluid 250 injected from the effluent (221) from the additional one or more standpipes. The reaction effluent from the additional standpipe (2 10) 131895.doc -36-

Claims

200911975 十、申請專利範圍： 1. 一種由輕汽油（C5-，其係使用一包含一種用於由重催化裂化饋料及至少 1 50 c)構成之輕饋料產生丙烯之方法下列各物之反應區：200911975 X. Patent application scope: 1. A method for producing propylene from light gasoline (C5-, which uses a light feed comprising a heavy catalytic cracking feedstock and at least 150 c) Area:

•一進行該重饋料之催化裂化之主要反應器⑽” …或多個在比該主要⑽高之嚴格度下操作且進灯輕饋料之催化裂化的額外豎管（21〇)，該或該等額外豎管⑽)與該主要賢管⑽平行操作，且將來自該或該等額外S管（2H))之氣態及固態排出物傳送至該主要反應器（100)之稀釋區（11〇)，在該方法中： a) 至少鳩且較佳地至少_之驟冷流體（1〇5)係由與來自該或該等額外豎管（21〇)之排出物（221)一起注射之驟冷流體（230)構成；且 b) 位於該稀釋區（110)上部之至少7〇%、較佳地至少8〇% 之沖洗流體（104)係由源自該或該等額外豎管（21〇)之反應排出物（221)構成。 2.如請求項1之用於由重催化裂化饋料及由輕汽油（c5_ 15〇°C)構成之輕饋料產生丙烯之方法，其中將來自該或 «亥專額外丑管（21 〇)之排出物初始分離為一含有該等反應排出物（221)之主要氣相，及一含有裂化催化劑（222)之主要固相，將該氣相傳送至該主要反應器（1〇〇)之稀釋區 (110)，且將該固相傳送至該主要反應器（1〇〇)之緻密區 (121)。 3.如請求項1之用於由重催化裂化饋料及由輕汽油（(：5_ 131895.doc 200911975 15〇。〇構成之輕饋料產生丙缔之方法，纟中該主要賢管及該或該等額外賢管中之流動為一垂直下向流。 4.如請求们之用於由重催化裂化饋料及由輕汽油（c5_ 1赃）構成之輕饋料產生丙歸之方法，其中由汽提蒸氣，）及（12G)及解吸附之煙構成的氣體全部通過汽提腔室（3 )之開口（26)，且具有在！ _至5 m/s範圍内、較佳杜5至4 m/s範圍内之通過該等開口（26)之向上流速。 5 士貝1之用於由重催化裂化饋料及由輕汽油（〇- 構成之輕饋料產生丙埽之m中該主要反應 -()之稀釋相（11Q)之溫度（T5)在49G°C至520。〇之範圍内。 6·如請求項1之用於由重催化裂化饋料及由輕汽油. 15〇°C)構成之輕饋料產生丙烯之方法，丨中自將該重饋料;引a主要豎官（1())之底部至自該主要反應器（⑽)排出/等反應排出物之出口所量測的該等試劑之滯留時間小於1 0秒。 7 . 如清求項1之用*ίρ/v rU壬' 用於由重催化裂化饋料及由輕汽油（C5_ 1 5 0 C )構成之輕餹斗斗連& $ # ^ 躀枓產生丙烯之方法，其中該等額外豎 \ 夕者的饋料為含有至少30重量％烯烴之輕館刀:、中^少80〇/〇之分子具有小於340。。之沸點。 :长項I之用於由重催化裂化饋料及由輕汽油（C5- μ )構成之輕饋料產生丙烯之方法，其中該等額外豎官中之至少~去& # + 者的饋枓為產生於該主要豎管中且含有少30%歸烴之輕汽油（c5⑽。以 131895.doc 200911975 9.如凊未項1之 ?輕汽油（C5-’該等額外登之輕C4或C5 輕汽油（C5-該等額外豎或植物油與 <用於由重催化裂化饋】50。〇構成之址寸+及 J再战之h饋料產生丙烯之方法，管t之至少—去从她，丨』者的饋料為由源自該主要& A 烯烴產生之寡聚汽油。丑1 ι〇·如請求項】之用於由重催化裂化饋料及由 C)構成之輕饋料產生丙烯之方法，其中执至夕者的饋料為植物油或動物脂肪動物脂肪之任何混合物。 131895.doc• a primary reactor (10)” for performing catalytic cracking of the heavy feedstock” or a plurality of additional risers (21〇) operating at a higher stringency than the primary (10) and catalytically cracked into the light feedstock, Or the additional standpipe (10)) operates in parallel with the main stalk (10) and delivers gaseous and solid effluent from the or additional S pipe (2H) to the dilution zone of the primary reactor (100) ( 11〇), in the method: a) at least, and preferably at least, the quenching fluid (1〇5) is from the effluent (221) from the or the additional standpipe (21〇) The injected quench fluid (230) is constructed; and b) at least 7%, preferably at least 8%, of the flushing fluid (104) located in the upper portion of the dilution zone (110) is derived from the or the additional vertical The reaction effluent (221) of the tube (21 构成) is composed of 2. The method of claim 1 for producing propylene from a heavy catalytic cracking feed and a light feed composed of light gasoline (c5_ 15 〇 ° C), wherein The effluent from the or _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ _ And a main solid phase containing the cracking catalyst (222), the gas phase is sent to the dilution zone (110) of the main reactor (1), and the solid phase is transferred to the main reactor (1〇〇) The dense area (121). 3. The method of claim 1 for the production of propylene by the heavy catalytic cracking feed and by the light gasoline ((: 5_131895.doc 200911975 15〇. The flow in the main sage and the or the other sages is a vertical downward flow. 4. The light feed for the heavy catalytic cracking feed and light gasoline (c5_ 1 赃) as requested by the requester. A method of producing a gamma, wherein the gas consisting of stripping steam, and (12G) and desorbed smoke all passes through the opening (26) of the stripping chamber (3) and has a range of _ to 5 m/s The upward flow rate through the openings (26) in the range, preferably in the range of 5 to 4 m/s. 5 士贝1 is used for the heavy catalytic cracking feed and the light feedstock composed of light gasoline (〇-) The temperature (T5) of the diluted phase (11Q) of the main reaction-() in the m-producing m is in the range of 49 G ° C to 520 〇. Item 1 is a method for producing propylene from a lightly fed material consisting of a heavy catalytic cracking feed and a light gasoline. 15 〇 ° C), from which the heavy feed is fed; a main vertical (1 ()) The residence time of the reagents measured from the bottom to the outlet of the main reactor ((10)) for discharge/equal discharge is less than 10 seconds. 7. For the use of item 1 *ίρ/v rU壬' a method for producing propylene from a heavy catalytic cracking feed and a lightly smashed bucket & $ # ^ 构成 consisting of light gasoline (C5_150C), wherein the additional erector feeds contain at least The light weight knife of 30% by weight of olefins has a molecular weight of less than 340. . The boiling point. : Long item I for the production of propylene from a heavy catalytic cracking feed and a light feed composed of light gasoline (C5-μ), wherein at least the ~~&## of the additional verticals For the light gasoline produced in the main standpipe and containing less than 30% of the hydrocarbons (c5 (10). To 131895.doc 200911975 9. If not the light gasoline (C5-' such additional light C4 or C5 Light gasoline (C5 - these additional vertical or vegetable oils and <for feeding by heavy catalytic cracking) 50. The method of 〇及及及及及及及及及及及及及及及及及及及及及及及及Her, 馈's feed is an oligomeric gasoline derived from the main & A olefin. Ugly 1 ι〇· as requested for light feedstock consisting of heavy catalytic cracking feedstock and C) A method of producing propylene, wherein the feed to the evening is any mixture of vegetable oil or animal fat animal fat.